AU728011B2 - Fluidized bed process for producing alumina from aluminum hydroxide - Google Patents
Fluidized bed process for producing alumina from aluminum hydroxide Download PDFInfo
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- AU728011B2 AU728011B2 AU74970/96A AU7497096A AU728011B2 AU 728011 B2 AU728011 B2 AU 728011B2 AU 74970/96 A AU74970/96 A AU 74970/96A AU 7497096 A AU7497096 A AU 7497096A AU 728011 B2 AU728011 B2 AU 728011B2
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- Prior art keywords
- fluidized bed
- solids
- aluminum hydroxide
- exhaust gas
- bed reactor
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- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 title claims abstract description 30
- 238000000034 method Methods 0.000 title claims abstract description 26
- 230000008569 process Effects 0.000 title claims abstract description 26
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 title claims abstract description 18
- 239000007787 solid Substances 0.000 claims abstract description 57
- 239000000725 suspension Substances 0.000 claims abstract description 44
- 239000000203 mixture Substances 0.000 claims abstract description 9
- 239000007788 liquid Substances 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 description 53
- 238000001816 cooling Methods 0.000 description 17
- 238000001354 calcination Methods 0.000 description 10
- 239000000463 material Substances 0.000 description 6
- 238000002156 mixing Methods 0.000 description 5
- 238000004064 recycling Methods 0.000 description 5
- 239000000446 fuel Substances 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000012798 spherical particle Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F7/00—Compounds of aluminium
- C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
- C01F7/44—Dehydration of aluminium oxide or hydroxide, i.e. all conversions of one form into another involving a loss of water
- C01F7/441—Dehydration of aluminium oxide or hydroxide, i.e. all conversions of one form into another involving a loss of water by calcination
- C01F7/445—Dehydration of aluminium oxide or hydroxide, i.e. all conversions of one form into another involving a loss of water by calcination making use of a fluidised bed
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Inorganic Chemistry (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Compositions Of Oxide Ceramics (AREA)
- Cold Cathode And The Manufacture (AREA)
- Inorganic Insulating Materials (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
PCT No. PCT/EP96/04764 Sec. 371 Date Sep. 3, 1998 Sec. 102(e) Date Sep. 3, 1998 PCT Filed Nov. 2, 1996 PCT Pub. No. WO97/18165 PCT Pub. Date May 22, 1997A process is disclosed for preparing anhydrous alumina from aluminum hydroxide which comprises feeding aluminum hydroxide into a first suspension preheater and partially dehydrating the aluminum hydroxide with a hot exhaust gas, transporting the partially dehydrated aluminum hydroxide with said exhaust gas to a first separating means and separately withdrawing the exhaust gas and the partially dehydrated aluminum hydroxide, and dividing the partially dehydrated aluminum hydroxide into a first and second partial stream of solids. The process uses a circulating fluidized bed comprising a fluidized bed reactor, a recycle separator connected to the upper portion of said fluidized bed reactor, and a return line for leading solids from said recycle separator to the lower portion of said fluidized bed reactor. The second partial stream of solids is fed into a second suspension preheater and contacted with hot exhaust gas from the recycle separator. The solids and the exhaust gas are transported to a second separating means and an exhaust gas stream is withdrawn and fed into the first suspension preheater. A dehydrated solids stream is fed into the fluidized bed reactor and the reactor temperature is adjusted to 850 to 1000 DEG C. A third partial stream of solids is mixed with the first partial stream of solids to form a hot solids mixture. The hot solids mixture is cooled in at least one fluidized bed cooler and then is fed into the fluidized bed reactor. The hot solids mixture is cooled in at least one fluidized bed cooler.
Description
FLUIDIZED BED PROCESS FOR PRODCUING ALUMINA FROM ALUMINUM
HYDROXIDE
BACKGROUND OF THE INVENTION This invention relates to a process of preparing anhydrous alumina from aluminum hydroxide in a circulating fluidized bed.
A known process is described in DE-A-1592140 which comprises a fluidizedbed reactor, a separator, and a return line, where the aluminum hydroxide is introduced into a first suspension preheater operated by means of the exhaust gases of the fluidized-bed reactor of the circulating fluidized bed, and is at least partially dehydrated, dehydrated aluminum hydroxide from the first suspension preheater is introduced into a second suspension pre-heater operated by means of the exhaust gases of the fluidized-bed reactor of the circulating fluidized bed, and is furthermore dehydrated and then supplied to the circulating fluidized bed, which is operated by means of oxygen-containing fluidizing gas indirectly heated in a subsequent cooling 15 stage by the alumina produced, and by means of directly heated, oxygen-containing secondary gas supplied at a higher level, where the indirect heating of the fluidizing gas is effected in a fluidized-bed cooler.
As against the known processes using a rotary kiln and the processes carried out in a fluidized bed, the above-stated process is in particular characterized by favorable heat consumption values of about 720 to 800 kcal/kg, which depending on :0the quality of the alumina produced are considerably lower than the typical values for rotary kilns in the range from 1000 to 1100 kcal/kg. These values are on the one "i hand reached as a result of a near-stoichiometric combustion of the fuel and the substantial utilization of the waste heat of the exhaust gases, which leave the calcining zone, for predrying and partial dehydration. On the other hand, the recirculation of the heat of the calcined material to the calcining zone in the form of the fluidizing gas and the secondary gas heated in the fluidized-bed cooler represents a substantial contribution to the reduction of the heat consumption values. A further advantage of the process consists in that due to the stepwise combustion, namely at first only by means of fluidizing air understoichiometrically in 2 the range of a high dispersion density, and then in the presence of secondary air stoichiometrically or slightly overstoichiometrically in the range of a low suspension density, an overheating which would impair the quality of the product made by such process is definitely avoided.
What is disadvantageous in the above-described process is the fact that at the generally required high calcining temperatures of 1000 to 11000C it is difficult to utilize the product heat in the actual calcining process. Either the gas streams required for a sufficient cooling of the product are so large that they cannot be completely used in the calcining process, or--in the case of a cooling against the gas streams required for the calcining process--the cooling of the product is not sufficient. Finally, the demands concerning the quality of the final calcined alumina have changed recently. What is desired in particular is an alumina of sandy quality, i.e. a high content of gamma-oxide. The changed requirements necessitate a considerable change in the execution of such process.
The above prior art is not admitted as common general knowledge.
OBJECT OF THE INVENTION An object of the present invention is to overcome or at least ameliorate at least one of the problems in the prior art, or to provide an alternative thereto.
A preferred object of the invention is to provide a process for preparing anhydrous alumina from aluminum hydroxide, which satisfies the changed requirements concerning the oxide quality, and in particular has a minimum consumption of heat.
SUMMARY OF THE INVENTION According to the present invention, there is provided a process for preparing anhydrous alumina from aluminum hydroxide which includes the steps of: feeding aluminum hydroxide into a first suspension preheater and contacting the aluminum hydroxide therein with a hot exhaust gas to partially dehydrate the aluminum hydroxide, transporting the partially dehydrated aluminum hydroxide with said exhaust gas to a first separating means and separately withdrawing from said first separating means the exhaust gas and the partially dehydrated aluminum hydroxide, dividing the partially dehydrated aluminum hydroxide into a first and second partial stream of solids, said first partial stream of solids amounting to 10 to 25% by weight of the aluminum hydroxide leaving the first suspension preheater; providing a circulating fluidized bed system including a fluidized bed reactor, supplied with fuel and with air as a fluidizing gas, a recycle separator connected to the upper portion of said fluidized bed reactor, and a return line for leading solids from said recycle separator to the lower portion of said fluidized bed reactor; feeding said second partial stream of solids into a second suspension preheater and contacting said second partial stream of solids therein with hot exhaust gas from said recycle separator connected to said fluidized bed reactor, transporting the solids and the exhaust gas from the second suspension preheater to S a second separating means and separately withdrawing from said second separating means an exhaust gas stream which is fed into the first suspension preheater and an at least partially dehydrated solids stream which is fed into the fluidized bed reactor, combusting said fuel in said fluidized bed reactor, and adjusting the temperature in said fluidized bed reactor in a range of 850 to 1000C; withdrawing a third partial stream of solids from the solids being 20 separated in the recycle separator and mixing said third partial stream of solids with .i.o said first partial stream of solids for at least 2 minutes to form a hot solids mixture; and feeding said hot solids mixture formed in step into a multi-stage suspension cooler and therein cooling said hot solids mixture in direct contact with air, withdrawing air from said multi-stage suspension cooler and feeding the air into the fluidized bed reactor as secondary air, then indirectly cooling said hot solids mixture with air in at least one fluidized bed cooler and feeding the air from the fluidized bed cooler into said fluidized bed reactor as said fluidizing gas, and withdrawing anhydrous alumina from said fluidized bed cooler.
IL
4 Preferably, according to step pressure loss in the fluidized bed reactor is adjusted to less than 100 mbar.
Preferably, according to step following discharge from the first separating means the exhaust gas is passed through an electrostatic filter and solids separated in said filter are added to the partially dehydrated aluminum hydroxide separated in said first separating means.
Preferably, according to step the fluidized bed cooler is also multi-staged and the solids mixture from the multi-stage suspension cooler is at first passed through a first fluidized bed indirectly cooled with air and then through a second fluidized bed indirectly cooled with a liquid heat transfer medium.
In an embodiment of the invention, with regard to the drawing, the process is carried out such that the temperature of the circulating fluidized bed is adjusted to a value in the range from 850 to 10000C, the alumina withdrawn from the circulating fluidized bed is mixed for at least 2 minutes with 10 to 25 wt-% of the partially dehydrated aluminum hydroxide leaving the first stage in the direction of solid flow of *the first suspension preheater 2, and the mixed material is cooled first in a multistage suspension cooler 15, 16, 17, 18, 19, 20 by heating secondary gas 11, and then in a fluidized-bed cooler 23 by indirectly heating fluidizing gas The system of the circulating fluidized bed used in the process in accordance 20 with an embodiment of the invention includes a fluidized-bed reactor, a separator for separating solids from the suspension discharged from the fluidized-bed reactorgenerally a recycling cyclone--and a return line for returning the separated solids to S" the fluidized-bed reactor. The principle of the circulating fluidized bed is characterized in that in contrast to the known fluidized bed, where a dense phase is separated from the gas space disposed above the same by a considerable density difference, there are states of distribution without a defined boundary layer. A density difference between the dense phase and the dust space disposed above the same does not exist, but the concentration of solids inside the reactor decreases from the bottom to the top. From the upper portion of the reactor a gas-solids suspension is discharged. When defining the operating conditions by means of the characteristics of Froude and Archimedes, the following ranges are obtained: 0. 1 3/4 Fr 2 Pk Pg or 0.01 Ar 100, where dAr k dg(pk Pg) Ar- *15 pg V 2 and 20 2 2 U Fr dk *go *o In the formulae: u is the relative gas velocity in m/sec Ar is the Archimedes number Fr is the Froude number p, is the density of the gas in kg/m 3 p, is the density of the solid particle in kg/m 3 dk is the diameter of the spherical particle in m u is the kinematic viscosity in m 2 /sec g is the gravitational constant in m/sec 2 The mixing of the solid streams, derived on the one hand via the by-pass line from the second suspension preheater in the direction of solid flow, and on the other
I.
6 hand from the circulating fluidized bed, for at least 2 minutes is essential for this process. Only then, a sufficient separation of the chemically bound water, which is still contained in the at least partially dehydrated aluminum hydroxide is achieved, and thus a sufficiently low loss of ignition is ensured. The mixing of the solid streams may be effected particularly advantageously by the steam produced during mixing.
The fluidizing gas velocity upstream of the secondary gas inlet may generally lies in the range from 7 to 10 m/sec.
An advantageous embodiment of the invention consists in that the pressure loss in the fluidized-bed reactor, which is a function of the solids content, is adjusted to <100 mbar.
In accordance with a further advantageous embodiment of the invention the partially dehydrated aluminum hydroxide leaving the first suspension preheater 2 is separated in a separator disposed before the electrostatic filter.
In accordance with a further embodiment of the invention, finally, it is advantageous that the final cooling of the alumina produced is effected by a multistage fluidized-bed cooling, where through an indirect heat exchange in the first stage the fluidizing gas for the fluidized-bed reactor of the circulating fluidized bed, and in the subsequent stages a liquid heat transfer medium is heated. In this way, the amount of air used for cooling the calcined material can most easily be adapted 20 to the amount of fluidizing air required by the fluidized-bed reactor of the circulating fluidized bed.
The outstanding advantage of the process in accordance with an embodiment of the invention consists in that the calcining process including preheating and cooling can most easily be adapted to the respective quality demands. For it is a known practice to require a certain product quality as regards BET surface, loss of ignition and oxide. This leads to the reaction temperature to be adjusted in the circulating fluidized bed and the amount of merely dehydrated aluminum hydroxide to be passed by the circulating fluidized bed as a by-pass. This means that with increasing BET surface both the calcining temperature in the circulating fluidized bed and the by-pass quantity for aluminum hydroxide must be adjusted towards the lower 7 limit values claimed. On the other hand, with decreasing BET surface the aforementioned values must be shifted towards the upper limit values claimed. In the case of an admissible increased loss of ignition the by-pass quantity for aluminum hydroxide can furthermore be increased within the claimed limits under otherwise constant operating conditions, in particular at a constant calcining temperature. In this way, a further reduction of the heat consumption value can be achieved.
A further advantage of the process in accordance with an embodiment of the invention consists in a heat consumption value, which depending on the quality demands to be met by the alumina produced is considerably below the so far usual values.
BRIEF DESCRIPTION OF THE DRAWING oleo An embodiment of the invention will now be explained in further detail, by way of example only, with reference to the Figure and the Example.
The FIGURE is a flow diagram of the process in accordance with an embodiment of the invention.
DETAILED DESCRIPTION OF EXEMPLARY EMBODIMENT The filter-moist aluminum hydroxide is introduced by means of a screw conveyor 1 into the first suspension preheater 2, and is entrained by the exhaust gas stream coming from the second suspension preheater 5. Subsequently the gas/material stream is separated in the subsequent cyclone separator 3.
The exhaust gas discharged from the cyclone separator 3 is supplied to an electrostatic gas cleaning unit 4 for the purpose of dedusting and then to a chimney (not shown).
The solid matter leaving the cyclone separator 3 and the electrostatic gas cleaning unit is then for the larger part supplied by a metering device to the second suspension preheater 5, and for the smaller part to the by-pass line 14. In the second suspension preheater 5 the solid matter is entrained by the exhaust gas leaving the recycling cyclone 6 of the circulating fluidized bed and is furthermore dewatered or dehydrated. In the separating cyclone 7 there is again effected a separation of the gas/material stream, where the dehydrated material is supplied to the fluidized-bed reactor 8, and the exhaust gas is passed into the above-mentioned suspension preheater 2.
The supply of the fuel required for calcining is effected via line 9, which is disposed at a small height above the grid of the fluidized-bed reactor 8. The oxygencontaining gas streams required for combustion are supplied as fluidizing gas via line and as secondary gas via line 11. Since the gas is supplied in the form of fluidizing gas and secondary gas, a comparatively high suspension density is achieved in the lower part of the reactor between grid and secondary gas inlet 11, and upstream of the secondary gas inlet 11 a comparatively low suspension density is achieved.
The gas-solids suspension is introduced into the recycling cyclone 6 of the circulating fluidized bed via the connecting line 12, in that a further separation of solids and gas is effected. The solids leaving the recycling cyclone 6 via line 13 are mixed with a part of the solids originating from the cyclone 3 and the electrostatic gas cleaning unit, which are supplied via line 14, and are supplied to the first suspension cooler comprising the riser 15 and the cyclone separator 16. The exhaust gas of the cyclone separator flows through line 11 into the fluidized-bed reactor 8, the solids are supplied to the second suspension cooler comprising the 20 riser 17 and the cyclone separator 18, and then to the third suspension cooler comprising the riser 19 and the cyclone separator 20. The gas flow through the individual suspension coolers is effected countercurrently to the solids via lines 21 and 22. Upon leaving the last suspension cooler, the alumina produced is subjected to a final cooling in the fluidized-bed cooler 23 equipped with three cooling chambers. In the first chamber the fluidizing gas supplied to the fluidized-bed reactor 8 is heated, and in the subsequently connected two chambers there is effected a cooling against a heat-transfer medium, preferably water, which flows countercurrently. The alumina is finally discharged via line 24.
EXAMPLE:
9 By means of the screw conveyor 1 the first suspension preheater 2 is supplied with 126,360 kg/h aluminum hydroxide containing 7 wt-% mechanically bound water.
By means of the exhaust gas supplied from the cyclone separator 7 at a temperature of 3060 C a first drying is effected. Upon separation in the cyclone separator 3, the solids are subjected to a further drying and dehydration in the second suspension preheater 5 by means of the exhaust gases supplied from the recycling cyclone 6 of the circulating fluidized bed at a temperature of 9500C The exhaust gas leaving the cyclone separator 3 is then dedusted in the electrostatic filter 4 and supplied to the chimney. Its quantity is 132,719 Nm 3 The solids produced in the cyclone separator 7 are then introduced into the fluidized-bed reactor 8 of the circulating fluidized bed.
9~l The circulating fluidized bed is operated at a temperature of 9500C Via line 9 it is supplied with 5,123 kg/h fuel oil, via line 11 with 60,425 Nm 3 /h secondary air, and via line 10 with 12,000 Nm 3 /h fluidizing air. The fluidizing air has a temperature of 15 1880C, and the secondary air has a temperature of 5250C. A gas stream in an amount of 98,631 Nm 3 /h with an oxygen content of 2.23 which is supplied to the suspension preheaters 5 and 2, as well as solids in the amount of 66,848 kg/h are leaving the circulating fluidized-bed. Before entering the riser 15 of the first 9 9 suspension cooler, this stream of solids discharged via line 13 is mixed with 15,262 999999 9 9 20 kg/h solids supplied via line 14, where a mixing temperature of 6080C has been set.
•After its passage through the riser 15, the gas-solids suspension flows into the cyclone separator 16 and from there to the subsequent suspension coolers comprising the risers 17 and 19 and the cyclone separators 18 and 20, respectively.
In the three suspension coolers the solids are cooled step by step to 5250C, 4120C and 2740C, respectively. At the same time, the secondary gas stream supplied to the fluidized-bed reactor 8 via line 11 is heated to a temperature of 5250C. The suspension coolers are operated by means of the directly heated fluidizing air of the subsequent fluidized-bed cooler 23 and by means of process air supplied via line in an amount of 33,000 Nm 3 /h.
The final cooling of the solids is effected in the fluidized bed cooler 23, whose first chamber is supplied with 7,200 Nm 3 /h fluidizing air, and whose 2nd and 3rd chambers are each supplied with 7,000 Nm 3 /h fluidizing air. The temperatures of the solids, which were achieved in the individual chambers, are 2380C, 1350C and 830C.
The air used for cooling in the first chamber of the fluidized-bed cooler 23 in an amount of 12,000 Nm 3 which is supplied to the fluidized-bed reactor 8 as fluidizing air, is heated to a temperature of 1880C through an indirect heat exchange. In the second and third cooling chambers of the fluidized-bed cooler 23 the cooling water, which countercurrently to the solids flows through the cooling chambers in an amount of 350,000 kg/h, is heated from 400C to 490C. The fluidizing air leaving the fluidized-bed cooler 23 has a temperature of 1530C and is produced in an amount of 21,200 Nm 3 As mentioned above, it is supplied to the suspension cooler. 77,111 kg/h alumina with a loss of ignition of 0.5% and a BET surface of 70 m2/g are leaving the fluidized-bed cooler 23.
i 15 The terms "comprise", "comprises", "comprised" and "comprising" when used in this specification are taken to specify the presence of stated features, integers, steps or components but does not preclude the presence or addition of one or more other features, integers, steps, components or groups thereof.
The embodiments have been advanced by way of example only, and modifications are possible within the scope of the invention as defined by the appended claims.
4. 44.
Claims (3)
- 2. The process defined in claim 1 wherein according to step pressure loss in *o* the fluidized bed reactor is adjusted to less than 100 mbar.
- 3. The process defined in claim 1, wherein according to step following discharge from the first separating means the exhaust gas is passed through an electrostatic filter and solids separated in said filter are added to the partially dehydrated aluminum hydroxide separated in said first separating means.
- 4. The process defined in claim 1, wherein according to step the fluidized bed Oa Oa cooler is also multi-staged and the solids mixture from the multi-stage suspension oo e cooler is at first passed through a first fluidized bed indirectly cooled with air and then through a second fluidized bed indirectly cooled with a liquid heat transfer medium. A process for preparing anhydrous alumina from aluminum hydroxide substantially as hereinbefore described and illustrated with reference to the accompanying drawing. DATED THIS 10TH DAY OF OCTOBER, 2000 METALLGESELLSCHAFT AKTIENGESELLSCHAFT WATERMARK PATENT TRADEMARK ATTORNEYS 290 BURWOOD ROAD HAWTHORN VICTORIA 3122 AUSTRALIA SKP/RJS/MEH P1 3805AU00.DOC *fee
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19542309A DE19542309A1 (en) | 1995-11-14 | 1995-11-14 | Process for the production of aluminum oxide from aluminum hydroxide |
| DE19542309 | 1995-11-14 | ||
| PCT/EP1996/004764 WO1997018165A1 (en) | 1995-11-14 | 1996-11-02 | Process for producing aluminium oxide from aluminium hydroxide |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| AU7497096A AU7497096A (en) | 1997-06-05 |
| AU728011B2 true AU728011B2 (en) | 2001-01-04 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU74970/96A Expired AU728011B2 (en) | 1995-11-14 | 1996-11-02 | Fluidized bed process for producing alumina from aluminum hydroxide |
Country Status (17)
| Country | Link |
|---|---|
| US (1) | US6015539A (en) |
| EP (1) | EP0861208B1 (en) |
| JP (1) | JP2000512255A (en) |
| CN (1) | CN1085623C (en) |
| AT (1) | ATE209607T1 (en) |
| AU (1) | AU728011B2 (en) |
| BR (1) | BR9611386A (en) |
| CA (1) | CA2235706C (en) |
| DE (2) | DE19542309A1 (en) |
| DK (1) | DK0861208T3 (en) |
| EA (1) | EA000516B1 (en) |
| ES (1) | ES2169270T3 (en) |
| ID (1) | ID17589A (en) |
| IN (1) | IN186958B (en) |
| SK (1) | SK284481B6 (en) |
| UA (1) | UA48201C2 (en) |
| WO (1) | WO1997018165A1 (en) |
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| DE19805897C1 (en) * | 1998-02-13 | 1998-12-03 | Metallgesellschaft Ag | Final cooling of anhydrous alumina produced from aluminium hydroxide in fluidised bed with simple heat recovery |
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| WO2023229496A1 (en) * | 2022-05-24 | 2023-11-30 | Общество с ограниченной ответственностью "Объединенная Компания РУСАЛ Инженерно-технологический центр" | Device for heat treating aluminium hydroxide |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| FR1559441A (en) * | 1967-06-16 | 1969-03-07 | ||
| FR2313120A1 (en) * | 1975-06-03 | 1976-12-31 | Metallgesellschaft Ag | METHOD FOR PERFORMING ENDOTHERMAL PROCESSES |
| GB2019369A (en) * | 1978-04-20 | 1979-10-31 | Smidth & Co As F L | Improvements relating to the production of anhydrous alumina |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| DE1909039B2 (en) * | 1969-02-22 | 1973-01-04 | Metallgesellschaft Ag, 6000 Frankfurt | Fluidized bed cooler |
| NO791174L (en) * | 1978-04-20 | 1979-10-23 | Smidth & Co As F L | PROCEDURE FOR MANUFACTURE OF WATERLESS ALUMINUM OXIDES |
| DE3405298A1 (en) * | 1984-02-15 | 1985-09-05 | Klöckner-Humboldt-Deutz AG, 5000 Köln | SYSTEM AND METHOD FOR CONTINUOUSLY CALCINATING ALUMINUM HYDROXIDE |
| US4585645A (en) * | 1985-04-03 | 1986-04-29 | Aluminum Company Of America | Alpha alumina production in a steam-fluidized reactor |
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1995
- 1995-11-14 DE DE19542309A patent/DE19542309A1/en not_active Withdrawn
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1996
- 1996-02-11 UA UA98063070A patent/UA48201C2/en unknown
- 1996-04-03 IN IN608CA1996 patent/IN186958B/en unknown
- 1996-11-02 AU AU74970/96A patent/AU728011B2/en not_active Expired
- 1996-11-02 EP EP96937331A patent/EP0861208B1/en not_active Expired - Lifetime
- 1996-11-02 SK SK642-98A patent/SK284481B6/en not_active IP Right Cessation
- 1996-11-02 DK DK96937331T patent/DK0861208T3/en active
- 1996-11-02 AT AT96937331T patent/ATE209607T1/en not_active IP Right Cessation
- 1996-11-02 DE DE59608329T patent/DE59608329D1/en not_active Expired - Fee Related
- 1996-11-02 US US09/068,758 patent/US6015539A/en not_active Expired - Fee Related
- 1996-11-02 CN CN96199087A patent/CN1085623C/en not_active Expired - Lifetime
- 1996-11-02 JP JP09518539A patent/JP2000512255A/en not_active Ceased
- 1996-11-02 EA EA199800451A patent/EA000516B1/en not_active IP Right Cessation
- 1996-11-02 WO PCT/EP1996/004764 patent/WO1997018165A1/en active IP Right Grant
- 1996-11-02 CA CA002235706A patent/CA2235706C/en not_active Expired - Fee Related
- 1996-11-02 ES ES96937331T patent/ES2169270T3/en not_active Expired - Lifetime
- 1996-11-02 BR BR9611386-3A patent/BR9611386A/en not_active IP Right Cessation
- 1996-11-14 ID IDP963326A patent/ID17589A/en unknown
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR1559441A (en) * | 1967-06-16 | 1969-03-07 | ||
| FR2313120A1 (en) * | 1975-06-03 | 1976-12-31 | Metallgesellschaft Ag | METHOD FOR PERFORMING ENDOTHERMAL PROCESSES |
| GB2019369A (en) * | 1978-04-20 | 1979-10-31 | Smidth & Co As F L | Improvements relating to the production of anhydrous alumina |
Also Published As
| Publication number | Publication date |
|---|---|
| US6015539A (en) | 2000-01-18 |
| JP2000512255A (en) | 2000-09-19 |
| CA2235706C (en) | 2004-08-31 |
| CN1204302A (en) | 1999-01-06 |
| EA199800451A1 (en) | 1998-10-29 |
| DK0861208T3 (en) | 2002-03-25 |
| ID17589A (en) | 1998-01-15 |
| EA000516B1 (en) | 1999-10-28 |
| SK64298A3 (en) | 1999-07-12 |
| AU7497096A (en) | 1997-06-05 |
| EP0861208A1 (en) | 1998-09-02 |
| BR9611386A (en) | 2000-10-24 |
| WO1997018165A1 (en) | 1997-05-22 |
| UA48201C2 (en) | 2002-08-15 |
| SK284481B6 (en) | 2005-04-01 |
| EP0861208B1 (en) | 2001-11-28 |
| CN1085623C (en) | 2002-05-29 |
| CA2235706A1 (en) | 1997-05-22 |
| ATE209607T1 (en) | 2001-12-15 |
| DE19542309A1 (en) | 1997-05-15 |
| DE59608329D1 (en) | 2002-01-10 |
| ES2169270T3 (en) | 2002-07-01 |
| IN186958B (en) | 2001-12-22 |
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Owner name: OUTOKUMPU OYJ Free format text: FORMER OWNER WAS: METALLGESELLSCHAFT AKTIENGESELLSCHAFT |